US3230246A - Process for preparing olefinically unsaturated nitriles - Google Patents

Process for preparing olefinically unsaturated nitriles Download PDF

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US3230246A
US3230246A US240733A US24073362A US3230246A US 3230246 A US3230246 A US 3230246A US 240733 A US240733 A US 240733A US 24073362 A US24073362 A US 24073362A US 3230246 A US3230246 A US 3230246A
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reactor
reaction
catalyst
trays
propylene
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US240733A
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James L Callahan
Ernest C Milberger
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Standard Oil Co
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Standard Oil Co
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Priority to IT708871D priority Critical patent/IT708871A/it
Priority to NL300817D priority patent/NL300817A/xx
Priority to CA742727A priority patent/CA742727A/en
Application filed by Standard Oil Co filed Critical Standard Oil Co
Priority to US240733A priority patent/US3230246A/en
Priority to GB40251/63A priority patent/GB981005A/en
Priority to ES293652D priority patent/ES293652A1/en
Priority to BR154668/63A priority patent/BR6354668D0/en
Priority to BE640435A priority patent/BE640435A/xx
Priority to FR955080A priority patent/FR1383210A/en
Priority to SE13099/63A priority patent/SE337814B/xx
Priority to DE19631468721 priority patent/DE1468721A1/en
Priority to LU44891D priority patent/LU44891A1/xx
Priority to AT952863A priority patent/AT252204B/en
Priority to CH1457263A priority patent/CH420118A/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/08—Silica
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/14—Phosphorus; Compounds thereof
    • B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C253/00—Preparation of carboxylic acid nitriles
    • C07C253/24—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
    • C07C253/26—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the present invention relates to an improvement in the process for the manufacture of an olefinically unsaturated nitrile by the reaction of ammonia and oxygen with an olefin, and more particularly, pertains to an improvement in the manufacture of an olefinically unsaturated nitrile such as acrylonitrile by a process which involves the catalytic vapor phase reaction of ammonia, oxygen and propylene in a plurality of reaction compartments.
  • the present process has special application to the production of acrylonitrile and methacrylonitrile from propylene and isobutylene, respectively.
  • the process comprises contacting a mixture comprising a monoolefin having from 3 to 4 carbon atoms such as propylene, ammonia and oxygen with a fluidized solid catalyst at an elevated temperature, at atmospheric or near atmospheric pressure in a plurality of semi-isolated fluidized beds.
  • the preferred reactants in this invention are a monoolefin having the structure wherein R is a member selected from the group consisting of hydrogen and a methyl radical such as propylene or isobutylene, ammonia, and oxygen. Any source of oxygen may be employed.
  • the molar ration of oxygen to olefin in the feed to the reaction vessel should be in the range of 0.5:1 to 3:1 and a ratio of about 1:1 to 2:1 is preferred.
  • the molar ratio of ammonia to olefin in the feed may vary between about 0.05 :1 to 5: 1. There is no real upper limit for the ammonia-olefin ratio, but there is generally no .point in exceeding the 5:1 ratio. At ammonia-olefin ratios appreciably less than the stoichiometric ratio of 1:1, various amounts of oxygenated derivatives of the olefin will be formed.
  • the molar ratio of water to olefin should be at least about 0.25:1. Ratios on the order of 1:1 are Patented Jan. 18, 1966 particularly desirable but higher ratios may be employed, i.e., up to about 10:1. Because of the recovery problems involved, it is generally preferred to use only so much water as is necessary to obtain the desired improvement in yield. It is to be understood that water does not behave only as a diluent in the reaction mixture, although the exact manner in which the water affects the reaction is not understood.
  • Any one or more of several catalysts which will function in the reaction between propylene, oxygen and ammonia to produce acrylonitrile are useful in the present process.
  • a particularly desirable group of catalysts for the purposes of the present process which are more fully disclosed in US. Patents Nos. 2,904,580; 3,044,966 and 3,050,546 are the bismuth, tin, and antimony salts of phosphomolybdic acid and molybdic acids, bismuth silicom-olybdate, bismuth silicophosphomolybdate, and hismuth phosphotungstate, and these a bismuth phosphomolybdate is preferred.
  • catalysts which are useful in the present invention include the combined oxides of bismuth and molybdenum, bismuth, molybdenum and optionally phosphorus, promoted by the addition of the oxides of barium and silicon, the combined oxides of antimony and uranium, antimony and iron, antimony and thorium, antimony and cerium, and antimony and manganese which are disclosed in the copending US. patent applications of I. L. Callahan, B. Gertisser and I. I. Szabo, Serial No. 190,038, filed April 25, 1962, and Serial No. 197,932, filed May 28, 1962, and those of J. L. Callahan and B. Gertisser, Serial Nos. 201,321 and 201,329, filed June 11, 1962 both now abandoned, and Serial Nos. 230,684; 230,717 and 230,741, filed October 15, 1962.
  • Still other catalysts which are useful in the process of the present invention are disclosed in Belgian Patents Nos. 592,434; 593,097; 598,511; 603,030; 612,136; 615,605 and 603,031, Canadian Patent No. 619,497, French Patent No. 1,278,289, British Patents Nos. 874,593 and 904,418, and US. Patent No. 2,481,826.
  • the catalysts useful in the present invention may be used alone or supported on or impregnated in a carrier material. Any suitable carrier material may be used, including silica, alumina, and the like. In general, the support will be employed in amounts less than by weight of the final catalyst composition.
  • the catalyst may be prepared by any of the numerous methods of catalyst preparation which are known to those skilled in the art.
  • the catalyst may be manufactured by co-gelling the various ingredients.
  • the co-gelled mass may be dried in accordance with conventional techniques.
  • the catalyst may be spray-dried, extruded as pellets or formed into spheres in oil as is well-known in the art.
  • the catalyst components may be mixed with a support in the form of a slurry followed by drying, or may be impregnated on silica or other support.
  • the catalyst may be prepared in any convenient form as, for instance, small particles suitable for use in the fluidized bed reactor.
  • a catalyst having a particle-size between 1 and 500 microns is preferred.
  • the temperature at which the reaction is carried out may be any temperature in the range of 550 to 1000 F.
  • the preferred temperature range is from about 800 to 950 F.
  • the pressure the which at reaction is conducted is also an important variable, and the reaction should be carried out at about atmospheric or slightly above atmospheric (2 to 3 atmospheres) pressure.
  • high pressures i.e., above 250 p.s.i.g., are not suitable for the process since higher pressures tend to favor the formation of undesirable by-products.
  • the apparent contact time employed in the process is not especially critical. Contact times in the range of 0.1 to 50 seconds may be employed.
  • the apparent contact time may be defined as the length of time in seconds which a unit volume of gas measured under the conditions of reaction is in contact with the apparent unit volume of catalyst. It may be calculated, for instance, from the apparent volume of the catalyst bed, the average'temperature and pressure of the reaction, and the flow rates in the vessel of the components of the reaction mixture.
  • the optimum contact time will, of course, vary depending upon the olefin being treated; but, in general, it may be said that a contact time of 1 to seconds is preferred.
  • any apparatus of the type suitable for carrying out reactions involving contacting vapors with a suspended powdered solid may be used in the present process.
  • the process may be carried out either continuously or intermittently.
  • the only requirement for the reactor used in the present invention is that it be made I I ziontally through the length of the column.
  • the perforations in the trays, gas velocities and particle size of the catalyst are sufficiently controlled to give a self-regulating type of reaction of optimum conversions and yields.
  • the process of the present invention produces unexpectedly superior results in comparison with the results obtained under the same conditions in a conventional single compartment fluidized catalyst apparatus wherein the single compartment has the same volume as the total com bined volumes of the multi-compartment reactor described above.
  • the reactor is preferably a flat, round or cone bottom tube constructed of metal, such as stainless steel, or other suitable material and closed at the bottom. Near to and up from the bottom of the tube there may be transversely mounted one or more reactant gas distribution grids or distribution spiders as is Well-known in the art. This distribution grid serves both as a catalyst support and as a sparging grid for air or oxygen which is introduced below the grid. A second sparger grid may be placed near the bottom of the reactor for dispersing the olefin and ammonia, if so desired. More details concerning the sparger grid may be found in US. Patents Nos. 2,893,849; 2,893,851 and 2,975,037.
  • the foraminous members which separate one communicating compartment from another in the reactor are generally mounted transversely within the reactor and may be screens, gratings, perforated plates, cones or pyriamid-al-shaped plates or one or more of the types, and arranged in one or more of the fashions, more fully disclosed in US. Patents Nos. 2,433,798; 2,730,556; 2,740,- 698; 2,823,219; 2,847,360; 2,893,849; and 2,893,851, as well as in the article appearing in the A. I. Ch. E. Journal, vol. 5, No. -1, pages 5460 (March 1959).
  • the types of openings in the foraminous members may be widely varied, the only requirement being that at least some of the openings be large enough to allow passage of the catalyst and reactants through them. More details concerning the numerous types and arrangement of openings in the foraminous members useful herein will be found in US. Patents Nos. 2,433,798; 2,740,698; 2,893,- 849; 2,893,851, and the aforementioned article appearing in the A. I. Ch. B. Journal. It is preferred that the openings in the foraminous members be rectangular, triangular, circular or oval in shape and that the size of the openings be within the limits of from 0.025 to 3 inches in diameter.
  • the amount of open area in the foraminous members may vary so long as it is within the limits of from 7.5 to 50% of the total internal cross-sectional area of the reactor.
  • the spacing of the foraminous members in the reactor is not a critical feature in the present process. Stated differently, it is not necessary that all of the communicating react-or compartments or chambers be of the same volume in the present process. Many types of spacing and arrangement of the foraminous members may be used and more details concerning spacing will be found in US. Patents Nos. 2,471,085; 2,- 823,219; 2,893,849 and 2,989,544.
  • the use of rotatable foraminous members, such as that disclosed in US. Patent No. 2,893,851 is within the scope of the process of the instant invention but is not a preferred embodiment.
  • the distance between any tWo foraminous members be at least about one inch and no greater than about three times the inside diameter of the reactor. It is more highly preferred for a given reaction compartment that the height be no greater than about twodiameters of the internal cross section of the compartment.
  • the catalyst fines often tend to be elutriated to some extent from the top of the reactor during the course of the reaction, it is convenient to expand the upper section of the reactor so that it acts as a disengaging section and it is often desira'ble to include at the top of the reactor means for recovering most or all of the catalyst fines as disclosed in US. Patents Nos. 2,494,614; 2,730,556; 2,893,849 and 2,- 893,851. After the aforementioned catalyst recovery it is also often convenient and even desirable to recycle the recovered catalyst fines through the reactor compartments by reintroducing them at a point near the bottom of the reactor as disclosed in US. Patents Nos.
  • the catalyst fines may be recovered and recycled, for instance, by employing a filter and one or more cyclones or centrifuges at the upper section of the reactor and a dip-leg for reintroducing the recovered catalyst into the bottom or near the bottom of the reactor.
  • the reactor may be brought to the reaction temperature before or after the introduction of the reaction feed mixture.
  • the reaction temperature In a large-scale operation it is preferred to carry out the process in a continuous manner, and in such a system the recirculation of the unreacted olefin is contemplated.
  • Periodic regeneration or reactivation of the catalyst is also contemplated, and this may generally be accomplished, for instance, by contacting the catalyst with air at an elevated temperature.
  • the reactor is, in essence, a sequence of several fluid beds with very limited back-flow of catalyst particles and vapor.
  • Each reaction compartment is a nearly perfectly stirred reactor in which the gases being contacted experience a very short average contact time. Because this contact time is short, contact time distribution is also very sharp. The effect of multiplying this short, sharp contact time over several reaction compartments in the instant novel process is to produce an overall contact time distribution which is much sharper than that which could be achieved in a single conventional fluid bed reactor of the same total reaction space.
  • the gaseous reactants may all be introduced into the reactor at once; they may be introduced separately or in various combinations, provided that they are eventually mixed and contacted with the fluidized catalyst in a plurality of communicating reaction compartments.
  • the products of the reaction may be recovered by any of the methods known to those skilled in the art.
  • One such method includes scrubbing the effiuent gases from the reactor with cold Water or an appropriate solvent to remove the products of the reaction.
  • the ultimate recovery of the products may be accomplished by conventional means.
  • the efficiency of the scrubbing operation may be improved when water is employed as the scrubbing agent by adding a suitable wetting agent to the water.
  • molecular oxygen is used as the oxidizing agent in this process, the resulting product mixture remaining after removal of the nitriles may be treated to remove carbon dioxide while the remainder of the mixture containing the unreacted propylene and oxygen may be recycled through the reactor.
  • the residual product after separation of the nitriles and the carbonyl products, may be scrubbed with a nonpolar solvent, e.g., a hydrocarbon fraction, in order to recover unreacted propylene or other hydrocarbons which may have been included in the feed or formed in the reaction, and in this case, the remaining gases may be discarded.
  • a nonpolar solvent e.g., a hydrocarbon fraction
  • the particular reactor employed was a 30inch length of schedule 40 stainless steel pipe having an inside diameter of 3 inches and enclosed at the bottom.
  • Near the bottom of the flat bottom reactor was a porous steel plate which served both as a catalyst support and as a sparging plate for air which was introduced into the reactor just below the sparging plate and below the point at which the propylene and ammonia were introduced.
  • the trays forming the compartments in the reactor were removable and were hung from a central /4 inch thermocouple well.
  • the plates were spaced at any desired interval with inch sleeves which slipped over the central thermocouple well.
  • a nut at the bottom of the well held the whole assembly tight.
  • the trays were cut circularly to fit with minimum clearance on the inside of the reactor. In operation, the entire reactor assembly was immersed in a temperature-controlled molten salt bath.
  • the eflluent from the top of the reactor was chilled in a stainless steel Ross exchanger and at the same time quenched with a flow of fresh water or hydrochloric acid solution.
  • the resulting condensate was collected in an ice-cooled receiver containing hydrochloric acid to neutralize excess ammonia.
  • Oif-gases from the first receiver were scrubbed in a second ice-cooled water scrubber and the non-condensables passed through a gas sampler bulb, and thence to a wet test gas meter.
  • a bismuth phosphomolybdate catalyst was prepared as follows:
  • a solution containing 9.3 cc. of phosphoric acid, 272 g. of molybdic acid (85% M00 40 cc. of nitric acid, and 582 g. of Bi(NO -5H O in 400 cc. of water was added to 750 g. of an aqueous colloidal silica sol containing 30% silica. The mixture was then evaporated to dryness and heated at 1000 F. for 16 hours. Subsequently, it was ground and screened to 40-100 mesh.
  • the foraminous members or trays used in this series of experiments were wire screen trays designated 9X9 mesh containing 0.069 inch holes with a total open area of 33% of the area of the reactor internal cross-section.
  • Constant conditions i.e-., a temperature of 900 F., a pressure of near atmospheric, and a mole ratio of feed of 10 air, 1 ammonia, and 1 water per mole of propylene were employed.
  • the variables, which were changed systematically, were contact time in the range of from 4 to 8 seconds and the numbr of trays (or compartments) in the reactor.
  • Example V An apparatus similar to that used in Example I having an internal diameter of 1 /2 inches was employed with and without perforated trays.
  • the perforated trays used each had inch holes and 30% open area.
  • eleven trays were used and they were uniformly spaced 1 /2 inches apart through the reactor.
  • the results of these experiments which were carried out in accordance with the procedure of Example I at a contact time of 7 seconds are given in Table V.
  • the feed mixture was a 10: 1:1.2:1 ratio of air:propylene:ammoniazwater, respectively.
  • Example V Percent conversion The procedure of Example V was repeated except that isobutylene was substitutde for propylene, four moles of water were used, a reaction temperature of 850 F. and
  • a process for preparing an olefinically unsaturated nitrile having the structure CHFCCN wherein R is a member selected from the group consisting of hydrogen and a methyl radical comprising contacting a mixture comprising a monoolefin having the structure wherein R has the foregoing designation, ammonia and oxygen with a fluidized solid catalyst at a temperature in the range of 550 to 1000 F. at from about atmospheric pressure up to about 250 p.s.i.g. in at least four communicating reaction compartments, each communicated with and being separated from the next adjacent one by a foraminous member.
  • the fluidized solid catalyst is a member selected from the group consisting of the bismuth, tin and antimony salts of phosphomolybdie acid; the bismuth, tin and antimony salts of molybdic acid; bismuth silicomolybdate; bismuth silicophosphomolybdate and bismuth phosphotungstate.

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  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
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Description

3,230,246 PRUCESS FOR PREPARING OLEFINICALLY UNSATURATED NITRILES James L. Cailahan, Redford, and Ernest C. Milberger,
Maple Heights, Chic, assignors to The Standard i] Company, Cieveiand, Ohio, a corporation of Ohio No Drawing. Filed Nov. 28, 1962, Ser. No. 240,733
Claims. (Ci. 260-4653) The present invention relates to an improvement in the process for the manufacture of an olefinically unsaturated nitrile by the reaction of ammonia and oxygen with an olefin, and more particularly, pertains to an improvement in the manufacture of an olefinically unsaturated nitrile such as acrylonitrile by a process which involves the catalytic vapor phase reaction of ammonia, oxygen and propylene in a plurality of reaction compartments. The present process has special application to the production of acrylonitrile and methacrylonitrile from propylene and isobutylene, respectively.
In its broadest aspect, the process comprises contacting a mixture comprising a monoolefin having from 3 to 4 carbon atoms such as propylene, ammonia and oxygen with a fluidized solid catalyst at an elevated temperature, at atmospheric or near atmospheric pressure in a plurality of semi-isolated fluidized beds.
The preferred reactants in this invention are a monoolefin having the structure wherein R is a member selected from the group consisting of hydrogen and a methyl radical such as propylene or isobutylene, ammonia, and oxygen. Any source of oxygen may be employed. The molar ration of oxygen to olefin in the feed to the reaction vessel should be in the range of 0.5:1 to 3:1 and a ratio of about 1:1 to 2:1 is preferred.
The presence of saturated hydrocarbons, propane or n-butane, for instance, in the feed mixture does not appear to influence the reaction to any appreciable degree and these materials appear to act only as diluents. Consequently, the presence of saturated hydrocarbons in the feed to the reactor is contemplated within the scope of this reaction. Similarly, other inert gaseous diluents such as nitrogen and the oxides of carbon may be present in the reaction mixtures Without deleterious effect.
The molar ratio of ammonia to olefin in the feed may vary between about 0.05 :1 to 5: 1. There is no real upper limit for the ammonia-olefin ratio, but there is generally no .point in exceeding the 5:1 ratio. At ammonia-olefin ratios appreciably less than the stoichiometric ratio of 1:1, various amounts of oxygenated derivatives of the olefin will be formed.
The presence of water in the feed mixture is within the scope of the present process. Improvements have been observed in reactions carried out in the presence of water as compared to similar runs made in the absence of added water. Consequently, the presence of water has a marked beneficial effect on this reaction, but reactions not including water in the feed are not meant to be excluded from this invention.
In general, the molar ratio of water to olefin should be at least about 0.25:1. Ratios on the order of 1:1 are Patented Jan. 18, 1966 particularly desirable but higher ratios may be employed, i.e., up to about 10:1. Because of the recovery problems involved, it is generally preferred to use only so much water as is necessary to obtain the desired improvement in yield. It is to be understood that water does not behave only as a diluent in the reaction mixture, although the exact manner in which the water affects the reaction is not understood.
Any one or more of several catalysts which will function in the reaction between propylene, oxygen and ammonia to produce acrylonitrile are useful in the present process. A particularly desirable group of catalysts for the purposes of the present process which are more fully disclosed in US. Patents Nos. 2,904,580; 3,044,966 and 3,050,546 are the bismuth, tin, and antimony salts of phosphomolybdic acid and molybdic acids, bismuth silicom-olybdate, bismuth silicophosphomolybdate, and hismuth phosphotungstate, and these a bismuth phosphomolybdate is preferred. Other catalysts which are useful in the present invention include the combined oxides of bismuth and molybdenum, bismuth, molybdenum and optionally phosphorus, promoted by the addition of the oxides of barium and silicon, the combined oxides of antimony and uranium, antimony and iron, antimony and thorium, antimony and cerium, and antimony and manganese which are disclosed in the copending US. patent applications of I. L. Callahan, B. Gertisser and I. I. Szabo, Serial No. 190,038, filed April 25, 1962, and Serial No. 197,932, filed May 28, 1962, and those of J. L. Callahan and B. Gertisser, Serial Nos. 201,321 and 201,329, filed June 11, 1962 both now abandoned, and Serial Nos. 230,684; 230,717 and 230,741, filed October 15, 1962.
Still other catalysts which are useful in the process of the present invention are disclosed in Belgian Patents Nos. 592,434; 593,097; 598,511; 603,030; 612,136; 615,605 and 603,031, Canadian Patent No. 619,497, French Patent No. 1,278,289, British Patents Nos. 874,593 and 904,418, and US. Patent No. 2,481,826.
The catalysts useful in the present invention may be used alone or supported on or impregnated in a carrier material. Any suitable carrier material may be used, including silica, alumina, and the like. In general, the support will be employed in amounts less than by weight of the final catalyst composition.
The catalyst may be prepared by any of the numerous methods of catalyst preparation which are known to those skilled in the art. For instance, the catalyst may be manufactured by co-gelling the various ingredients. The co-gelled mass may be dried in accordance with conventional techniques. The catalyst may be spray-dried, extruded as pellets or formed into spheres in oil as is well-known in the art. Alternatively, the catalyst components may be mixed with a support in the form of a slurry followed by drying, or may be impregnated on silica or other support. The catalyst may be prepared in any convenient form as, for instance, small particles suitable for use in the fluidized bed reactor. For the purpose of the present invention, a catalyst having a particle-size between 1 and 500 microns is preferred.
The temperature at which the reaction is carried out may be any temperature in the range of 550 to 1000 F. The preferred temperature range is from about 800 to 950 F.
The pressure the which at reaction is conducted is also an important variable, and the reaction should be carried out at about atmospheric or slightly above atmospheric (2 to 3 atmospheres) pressure. In general, high pressures, i.e., above 250 p.s.i.g., are not suitable for the process since higher pressures tend to favor the formation of undesirable by-products.
The apparent contact time employed in the process is not especially critical. Contact times in the range of 0.1 to 50 seconds may be employed. The apparent contact time may be defined as the length of time in seconds which a unit volume of gas measured under the conditions of reaction is in contact with the apparent unit volume of catalyst. It may be calculated, for instance, from the apparent volume of the catalyst bed, the average'temperature and pressure of the reaction, and the flow rates in the vessel of the components of the reaction mixture. The optimum contact time will, of course, vary depending upon the olefin being treated; but, in general, it may be said that a contact time of 1 to seconds is preferred.
In general, any apparatus of the type suitable for carrying out reactions involving contacting vapors with a suspended powdered solid may be used in the present process. The process may be carried out either continuously or intermittently. The only requirement for the reactor used in the present invention is that it be made I I ziontally through the length of the column. The perforations in the trays, gas velocities and particle size of the catalyst are sufficiently controlled to give a self-regulating type of reaction of optimum conversions and yields.
The process of the present invention produces unexpectedly superior results in comparison with the results obtained under the same conditions in a conventional single compartment fluidized catalyst apparatus wherein the single compartment has the same volume as the total com bined volumes of the multi-compartment reactor described above.
'The reactor is preferably a flat, round or cone bottom tube constructed of metal, such as stainless steel, or other suitable material and closed at the bottom. Near to and up from the bottom of the tube there may be transversely mounted one or more reactant gas distribution grids or distribution spiders as is Well-known in the art. This distribution grid serves both as a catalyst support and as a sparging grid for air or oxygen which is introduced below the grid. A second sparger grid may be placed near the bottom of the reactor for dispersing the olefin and ammonia, if so desired. More details concerning the sparger grid may be found in US. Patents Nos. 2,893,849; 2,893,851 and 2,975,037.
The foraminous members which separate one communicating compartment from another in the reactor are generally mounted transversely within the reactor and may be screens, gratings, perforated plates, cones or pyriamid-al-shaped plates or one or more of the types, and arranged in one or more of the fashions, more fully disclosed in US. Patents Nos. 2,433,798; 2,730,556; 2,740,- 698; 2,823,219; 2,847,360; 2,893,849; and 2,893,851, as well as in the article appearing in the A. I. Ch. E. Journal, vol. 5, No. -1, pages 5460 (March 1959).
The types of openings in the foraminous members may be widely varied, the only requirement being that at least some of the openings be large enough to allow passage of the catalyst and reactants through them. More details concerning the numerous types and arrangement of openings in the foraminous members useful herein will be found in US. Patents Nos. 2,433,798; 2,740,698; 2,893,- 849; 2,893,851, and the aforementioned article appearing in the A. I. Ch. B. Journal. It is preferred that the openings in the foraminous members be rectangular, triangular, circular or oval in shape and that the size of the openings be within the limits of from 0.025 to 3 inches in diameter.
The amount of open area in the foraminous members may vary so long as it is within the limits of from 7.5 to 50% of the total internal cross-sectional area of the reactor. For more details concerning the open area in the foraminous members useful in the present invention see US. Patents Nos. 2,433,798; 2,893,849 and 2,893,851.
As has been pointed out earlier and will be seen in the examples which follow, the spacing of the foraminous members in the reactor is not a critical feature in the present process. Stated differently, it is not necessary that all of the communicating react-or compartments or chambers be of the same volume in the present process. Many types of spacing and arrangement of the foraminous members may be used and more details concerning spacing will be found in US. Patents Nos. 2,471,085; 2,- 823,219; 2,893,849 and 2,989,544. The use of rotatable foraminous members, such as that disclosed in US. Patent No. 2,893,851, is within the scope of the process of the instant invention but is not a preferred embodiment. In any event, it is preferred that the distance between any tWo foraminous members be at least about one inch and no greater than about three times the inside diameter of the reactor. It is more highly preferred for a given reaction compartment that the height be no greater than about twodiameters of the internal cross section of the compartment.
It is often desirable and actually is preferred to include heat exchanger coils within the reactor compartments for better temperature control during the reaction. Such an arrangement is typified in U.S. Patents Nos. 2,676,668 and 2,893,851.
Because, as in most fluidized bed reactors, the catalyst fines often tend to be elutriated to some extent from the top of the reactor during the course of the reaction, it is convenient to expand the upper section of the reactor so that it acts as a disengaging section and it is often desira'ble to include at the top of the reactor means for recovering most or all of the catalyst fines as disclosed in US. Patents Nos. 2,494,614; 2,730,556; 2,893,849 and 2,- 893,851. After the aforementioned catalyst recovery it is also often convenient and even desirable to recycle the recovered catalyst fines through the reactor compartments by reintroducing them at a point near the bottom of the reactor as disclosed in US. Patents Nos. 2,494,614; 2,- 847,360 and in the aforementioned article appearing in the A. I. Ch. E. Journal. The catalyst fines may be recovered and recycled, for instance, by employing a filter and one or more cyclones or centrifuges at the upper section of the reactor and a dip-leg for reintroducing the recovered catalyst into the bottom or near the bottom of the reactor.
The reactor may be brought to the reaction temperature before or after the introduction of the reaction feed mixture. In a large-scale operation it is preferred to carry out the process in a continuous manner, and in such a system the recirculation of the unreacted olefin is contemplated. Periodic regeneration or reactivation of the catalyst is also contemplated, and this may generally be accomplished, for instance, by contacting the catalyst with air at an elevated temperature.
The reactor is, in essence, a sequence of several fluid beds with very limited back-flow of catalyst particles and vapor. Each reaction compartment is a nearly perfectly stirred reactor in which the gases being contacted experience a very short average contact time. Because this contact time is short, contact time distribution is also very sharp. The effect of multiplying this short, sharp contact time over several reaction compartments in the instant novel process is to produce an overall contact time distribution which is much sharper than that which could be achieved in a single conventional fluid bed reactor of the same total reaction space.
In accordance with the present invention, the gaseous reactants may all be introduced into the reactor at once; they may be introduced separately or in various combinations, provided that they are eventually mixed and contacted with the fluidized catalyst in a plurality of communicating reaction compartments.
The products of the reaction may be recovered by any of the methods known to those skilled in the art. One such method includes scrubbing the effiuent gases from the reactor with cold Water or an appropriate solvent to remove the products of the reaction. In such a case, the ultimate recovery of the products may be accomplished by conventional means. The efficiency of the scrubbing operation may be improved when water is employed as the scrubbing agent by adding a suitable wetting agent to the water. When molecular oxygen is used as the oxidizing agent in this process, the resulting product mixture remaining after removal of the nitriles may be treated to remove carbon dioxide while the remainder of the mixture containing the unreacted propylene and oxygen may be recycled through the reactor. When :air is employed as the oxidizing agent in lieu of molecular oxygen, the residual product, after separation of the nitriles and the carbonyl products, may be scrubbed with a nonpolar solvent, e.g., a hydrocarbon fraction, in order to recover unreacted propylene or other hydrocarbons which may have been included in the feed or formed in the reaction, and in this case, the remaining gases may be discarded. The addition of a suitable inhibitor to prevent polymerization of the unsaturated products during the recovery steps of the instant process is also contemplated.
In the examples, conventional auxiliary equipment, including meters, were employed for carrying out the reaction, and all the data reported herein are within the usual limits of experimental accuracy for such equipment. The products of the reactions were recovered by scrubbing the eiiiuent gases from the reactor with water or hydrochloric acid solutions. The products were analyzed by conventional means, including mass spectrographic, gas chromatographic, and infrared spectrometric analyses, as well as conventional titration where such analyses were applicable.
The particular reactor employed was a 30inch length of schedule 40 stainless steel pipe having an inside diameter of 3 inches and enclosed at the bottom. Near the bottom of the flat bottom reactor was a porous steel plate which served both as a catalyst support and as a sparging plate for air which was introduced into the reactor just below the sparging plate and below the point at which the propylene and ammonia were introduced. The trays forming the compartments in the reactor were removable and were hung from a central /4 inch thermocouple well. The plates were spaced at any desired interval with inch sleeves which slipped over the central thermocouple well. A nut at the bottom of the well held the whole assembly tight. The trays were cut circularly to fit with minimum clearance on the inside of the reactor. In operation, the entire reactor assembly was immersed in a temperature-controlled molten salt bath.
The eflluent from the top of the reactor was chilled in a stainless steel Ross exchanger and at the same time quenched with a flow of fresh water or hydrochloric acid solution. The resulting condensate was collected in an ice-cooled receiver containing hydrochloric acid to neutralize excess ammonia. Oif-gases from the first receiver were scrubbed in a second ice-cooled water scrubber and the non-condensables passed through a gas sampler bulb, and thence to a wet test gas meter.
Combined acidified aqueous scrubbing liquids were analyzed for acrylonitrile, as Well as small amounts of carbonyls, by gas chromatography. Excess ammonia was determined by back titration of the acidified scrubbing liquid and HCN was deter-mined by titration of this liquid also. The gas sample was analyzed chromatographically using the Fisher partitioner to give a direct measure of unreacted propylene, oxygen, carbon dioxide, and carbon monoxide.
Throughout this specification, the following definitions are employed:
Superficial linear gas velocity Vol. feed fU/sec.
Reactor height (1%.) Superficial linear gas velocity (ft/sec.)
Contact time:
Average linear gas velocity through the holes in the foraminous members (Percent, open area) (contact time) Percent conversions Weight of carbon in the product Weight of carbon in the propylene feed 100 Percent yield Weight of carbon in the product 100 Total weight of carbon in the converted propylene EXAMPLE I A bismuth phosphomolybdate catalyst was prepared as follows:
A solution containing 9.3 cc. of phosphoric acid, 272 g. of molybdic acid (85% M00 40 cc. of nitric acid, and 582 g. of Bi(NO -5H O in 400 cc. of water was added to 750 g. of an aqueous colloidal silica sol containing 30% silica. The mixture was then evaporated to dryness and heated at 1000 F. for 16 hours. Subsequently, it was ground and screened to 40-100 mesh.
The foraminous members or trays used in this series of experiments were wire screen trays designated 9X9 mesh containing 0.069 inch holes with a total open area of 33% of the area of the reactor internal cross-section.
Constant conditions, i.e-., a temperature of 900 F., a pressure of near atmospheric, and a mole ratio of feed of 10 air, 1 ammonia, and 1 water per mole of propylene were employed. The variables, which were changed systematically, were contact time in the range of from 4 to 8 seconds and the numbr of trays (or compartments) in the reactor.
A complete summary of these data is shown in Table I. The term useful products includes acrylonitrile and acetonitrile. Total conversion is based on conversion of propylene to all products including acrylonitrile, acetonitrile, HCN, CO and CO. Listed are results from experiments conducted in the foregoing manner in the aforementioned reactor with no trays (open fixed fluidized bed), 3 trays, 5 trays, and 11 trays. The total fluidized catalyst bed depth was maintained throughout these experiments at 18 inches. Spacing of the trays was symmetrical in the case of the 5 and 11 tray sieves. The three-tray configuration was an unsymmetrical arrangement with bottom and top trays up to 3 inches from the bottom and down 3 inches from the top respectively, with the third tray spaced intermediate between the two.
Table I Percent conversion Percent yield Contact useful time Acrylo- Useful Total products (sec.)
nitrile products No trays 47.0 51. 7 73. 8 70. 5 4 46. 7 50.8 70. 6 71. 7 5 50. 9 54. 5 72. 4 75. 3 6 53.0 56. 7 73. 6 77. 1 7 56. 5 59. 9 77.8 76.8 8 Three trays 50. 4 55. 6 74. 5 74. 8 4 53. 4 57. 3 73. 7 77. 7 5 58. 6 62. 2 78.3 79. 5 6 60. 2 63. 6 81. 6 78. 7 61. 9 64. 4 83. 4 77. 2 8 trays 59. 6 64. 5 80. 8 79.8 4 60. 5 66. 0 85. 5 77. 3 5 65.0 68. 7 89.1 77. 1 6 66. 1 70. 0 91. 5 76. 5 7 67.7 72.8 91. 8 79. 3 8 11 trays 62. 8 66. 9 81.4 82. 2 4 67. 5 74. 5 91. 5 81. 3 5 67.2 71. 0 91. 0 78.0 6 71. 1 74. 8 93. 2 80. 2 7 70. 1 74. 4 89. 4 83. 2 8
EXAMPLE II Two other tray types were tested at the S-tray level in the manner more fully described in Example I. The trays were inch thick steel plates cut to fit snugly inside of the reactor. One type of tray contained A inch in diameter circular holes, such that the total area. of the holes was equivalent to 13.2% of the total tray area. The scond tray type was a similar drilled plate, but the hole-size was 7 inch in diameter and the total open area was equal to 20% of the total tray area. Data for runs made in the reactor equipped with 5 trays and 11 trays, using each of these modifications are given in Table II.
Table 11 Percent conversion Percent yield Contact useful time Acrylo- Useful Total products (sec.)
nitrile products 5 tra s 1 ho1es 56.0 63. 4 78.3 81. 0 4 y A 62.4 66.4 84.9 78.2 5 63. 9 67.7 85. 8 79. 0 6 5 trays, Me" holes- 63. 1 69. 6 84. 4 82. 5 4 60. 8 66. 0 83. 9 78. 7 5 61. 2 68. 7 86. 5 79. 5 6 11 trays, %6
holes 64.0 71. 4 87.1 81. 9 4 63. 5 70.8 90. 8 78. 0 5 63. 2 70.2 91. 6 76. 7 6
It is apparent that the per pass conversion to acrylonitrile is not greatly dependent on tray hole-size and open areas within the range shown.
EXAMPLE III apart in the reactor for one acrylonitrile preparation.
The same 5 trays were then redistributed so that there was an open space of 8 inches between the air inlet sparging plate and the first tray (unsymmetrical). The remaining 4 trays were then crowded into the top inch space at a spacing of 2 inches. The results are given in Table III.
The per pass conversion to acrylonitrile, the principal desired product, increases with contact time rapidly to 5 seconds after which there is a distinct leveling (Table IV). The procedure outlined in Example I wherein an 11 inch tray reactor was employed was followed. The variation of contact time was studied and the results are given in Table Table IV Contact Percent conversion time per pass to (sec.) acrylonitrile EXAMPLE V A catalyst system composed of antimony oxide and uranium oxide, having an Sb:U atomic ratio of 8:1 was prepared as follows: g. of antimony metal was dis solved in 375 cc. of nitric acid (specific gravity of 1.42) and the mixture was heated until the evolution of oxides of nitrogen had ceased. To this solution was then added a suspension of 40.1 g. of uranyl acetate in 400 cc. of water. 300 cc. of ammonium hydroxide solution was then added, and the filtered reaction slurry was washed with 600 cc. of water in three 200 cc. portions. The filter cake was dried at C. overnight, calcined at 800 F. for 12 hours, and activated by heating at 1400 F. for 12 hours in a mufiie furnace open to the atmosphere.
An apparatus similar to that used in Example I having an internal diameter of 1 /2 inches was employed with and without perforated trays. The perforated trays used each had inch holes and 30% open area. In the reaction carried out in accordance with this invention, eleven trays were used and they were uniformly spaced 1 /2 inches apart through the reactor. The results of these experiments which were carried out in accordance with the procedure of Example I at a contact time of 7 seconds are given in Table V. The feed mixture was a 10: 1:1.2:1 ratio of air:propylene:ammoniazwater, respectively.
Table V Percent conversion The procedure of Example V was repeated except that isobutylene was substitutde for propylene, four moles of water were used, a reaction temperature of 850 F. and
a contact time of 6 seconds were employed. Much higher per pass conversions to methacrylonitrile were obtained in the 11 tray reactor than were obtained in the same reactor having no trays.
Results similar to the foregoing were obtained using as catalysts the combined oxides of antimony and iron, antimony and thorium, antimony and cerium and antimony and manganese.
We claim:
1. A process for preparing an olefinically unsaturated nitrile having the structure CHFCCN wherein R is a member selected from the group consisting of hydrogen and a methyl radical comprising contacting a mixture comprising a monoolefin having the structure wherein R has the foregoing designation, ammonia and oxygen with a fluidized solid catalyst at a temperature in the range of 550 to 1000 F. at from about atmospheric pressure up to about 250 p.s.i.g. in at least four communicating reaction compartments, each communicated with and being separated from the next adjacent one by a foraminous member.
2. The process of claim 1 wherein the unsaturated nitrile is acrylonitrile and the monoolefin is propylene.
3. The process of claim 1 wherein the unsaturated nitrile is methacrylonitrile and the monoolefin is isobutylene.
4. The process of claim 1 wherein the fluidized solid catalyst is a member selected from the group consisting of the bismuth, tin and antimony salts of phosphomolybdie acid; the bismuth, tin and antimony salts of molybdic acid; bismuth silicomolybdate; bismuth silicophosphomolybdate and bismuth phosphotungstate.
5. The process of claim 2 wherein the fluidized solid catalyst is bismuth phosphomolybdate.
References Cited by the Examiner UNITED STATES PATENTS 2,433,798 12/1947 Voorhees 196-52 2,471,085 5/1949 Wilcox et a1. 19652 2,823,219 2/1958 Mungen 260449.6 2,847,360 8/1958 Hemminger 1965O 2,904,580 9/1959 Idol 260--465.3 3,009,943 11/1961 Hadley et a1. 260465.3
CHARLES B. PARKER, Primary Examiner.

Claims (1)

1. A PROCESS FOR PREPARING AN OLEFINICALLY UNSATURATED NITRILE HAVING THE STRUCTURE
US240733A 1962-11-28 1962-11-28 Process for preparing olefinically unsaturated nitriles Expired - Lifetime US3230246A (en)

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US240733A US3230246A (en) 1962-11-28 1962-11-28 Process for preparing olefinically unsaturated nitriles
GB40251/63A GB981005A (en) 1962-11-28 1963-10-11 Process for preparing nitriles
ES293652D ES293652A1 (en) 1962-11-28 1963-11-19 Process for preparing olefinically unsaturated nitriles
BR154668/63A BR6354668D0 (en) 1962-11-28 1963-11-20 AN IMPROVEMENT IN THE PROCESS FOR CATALYTIC PREPARATION OF OLEFINICALLY Unsaturated NITRILLES FROM A MIXTURE CONTAINING OLEPHINE AMMONIUM AND OXYGEN CONTAINING OLEFINE AMMONIUM AND OXYGEN
BE640435A BE640435A (en) 1962-11-28 1963-11-26
FR955080A FR1383210A (en) 1962-11-28 1963-11-26 Process for the preparation of nitriles
SE13099/63A SE337814B (en) 1962-11-28 1963-11-27
DE19631468721 DE1468721A1 (en) 1962-11-28 1963-11-27 Process for the production of olefinically unsaturated nitriles
LU44891D LU44891A1 (en) 1962-11-28 1963-11-27
AT952863A AT252204B (en) 1962-11-28 1963-11-28 Process for the catalytic production of olefinically unsaturated nitriles
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US3427343A (en) * 1964-11-04 1969-02-11 Standard Oil Co Process for preparing olefinically unsaturated aldehydes and nitriles
US3883573A (en) * 1973-06-15 1975-05-13 Standard Oil Co Commercial fixed-bed acrylonitrile or methacrylonitrile
US3944592A (en) * 1970-05-22 1976-03-16 The Badger Company, Inc. Method of producing unsaturated nitriles
US3959341A (en) * 1972-09-25 1976-05-25 The B.F. Goodrich Company Process for low ammonia operation of the nitrile synthesis
US4082786A (en) * 1975-12-16 1978-04-04 Mitsubishi Gas Chemical Company, Inc. Process of production of aromatic nitriles
US4284583A (en) * 1979-10-29 1981-08-18 Uop Inc. Ammoxidation process with external catalyst regeneration zone
US4305886A (en) * 1979-08-13 1981-12-15 Uop Inc. Process for the ammoxidation of alkylaromatic hydrocarbons
US4338788A (en) * 1980-07-22 1982-07-13 Uop Inc. Cogeneration process linking FCC regenerator and power plant turbine
US5093299A (en) * 1990-01-09 1992-03-03 The Standard Oil Company Catalyst for process for the manufacture of acrylonitrile and methacrylonitrile
US5212137A (en) * 1990-01-09 1993-05-18 Standard Oil Company Catalyst for the manufacture of acrylonitrile and methacrylonitrile
US5840955A (en) * 1997-11-25 1998-11-24 Sockell; Edward J. Waste minimization and product recovery process
US6716405B1 (en) 1997-06-06 2004-04-06 China Petro-Chemical Corporation Process for removing unreacted ammonia from an effluent in a hydrocarbon ammoxidation reaction
BG64505B1 (en) * 1998-05-13 2005-05-31 The Standard Oil Co. Method for treatment of liquid process streams of acrylonitrile by means of oxidation reduction
EP1961736A1 (en) 1998-05-20 2008-08-27 Ineos Usa Llc Recovery of organics from process flare header
US20090299087A1 (en) * 2008-05-28 2009-12-03 Solutia, Inc. Process for manufacturing unsaturated mononitriles to improve on-stream time and reduce fouling
WO2011119207A1 (en) 2010-03-23 2011-09-29 Ineos Usa Llc Process for preparing improved mixed metal oxide ammoxidation catalysts
WO2011119203A1 (en) 2010-03-23 2011-09-29 Ineos Usa Llc High efficiency ammoxidation process and mixed metal oxide catalysts
WO2011119208A1 (en) 2010-03-23 2011-09-29 Ineos Usa Llc Improved mixed metal oxide ammoxidation catalysts
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WO2013043371A1 (en) 2011-09-21 2013-03-28 Ineos Usa Llc Mixed metal oxide catalysts
WO2015183284A1 (en) 2014-05-29 2015-12-03 Ineos Usa, Llc Improved selective ammoxidation catalysts
WO2015183283A1 (en) 2014-05-29 2015-12-03 Ineos Usa, Llc Improved selective ammoxidation catalysts
WO2018071166A1 (en) 2016-10-11 2018-04-19 Ineos Europe Ag Ammoxidation catalyst with selective co-product hcn production
US10676426B2 (en) 2017-06-30 2020-06-09 Novomer, Inc. Acrylonitrile derivatives from epoxide and carbon monoxide reagents
WO2023223295A1 (en) 2022-05-20 2023-11-23 Ineos Europe Ag Catalyst for the manufacture of acrylonitrile

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Cited By (25)

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Publication number Priority date Publication date Assignee Title
US3427343A (en) * 1964-11-04 1969-02-11 Standard Oil Co Process for preparing olefinically unsaturated aldehydes and nitriles
US3944592A (en) * 1970-05-22 1976-03-16 The Badger Company, Inc. Method of producing unsaturated nitriles
US3959341A (en) * 1972-09-25 1976-05-25 The B.F. Goodrich Company Process for low ammonia operation of the nitrile synthesis
US3883573A (en) * 1973-06-15 1975-05-13 Standard Oil Co Commercial fixed-bed acrylonitrile or methacrylonitrile
US4082786A (en) * 1975-12-16 1978-04-04 Mitsubishi Gas Chemical Company, Inc. Process of production of aromatic nitriles
US4305886A (en) * 1979-08-13 1981-12-15 Uop Inc. Process for the ammoxidation of alkylaromatic hydrocarbons
US4284583A (en) * 1979-10-29 1981-08-18 Uop Inc. Ammoxidation process with external catalyst regeneration zone
US4338788A (en) * 1980-07-22 1982-07-13 Uop Inc. Cogeneration process linking FCC regenerator and power plant turbine
US5093299A (en) * 1990-01-09 1992-03-03 The Standard Oil Company Catalyst for process for the manufacture of acrylonitrile and methacrylonitrile
US5212137A (en) * 1990-01-09 1993-05-18 Standard Oil Company Catalyst for the manufacture of acrylonitrile and methacrylonitrile
US6716405B1 (en) 1997-06-06 2004-04-06 China Petro-Chemical Corporation Process for removing unreacted ammonia from an effluent in a hydrocarbon ammoxidation reaction
US5840955A (en) * 1997-11-25 1998-11-24 Sockell; Edward J. Waste minimization and product recovery process
BG64505B1 (en) * 1998-05-13 2005-05-31 The Standard Oil Co. Method for treatment of liquid process streams of acrylonitrile by means of oxidation reduction
EP1961736A1 (en) 1998-05-20 2008-08-27 Ineos Usa Llc Recovery of organics from process flare header
US20090299087A1 (en) * 2008-05-28 2009-12-03 Solutia, Inc. Process for manufacturing unsaturated mononitriles to improve on-stream time and reduce fouling
WO2011119207A1 (en) 2010-03-23 2011-09-29 Ineos Usa Llc Process for preparing improved mixed metal oxide ammoxidation catalysts
WO2011119203A1 (en) 2010-03-23 2011-09-29 Ineos Usa Llc High efficiency ammoxidation process and mixed metal oxide catalysts
WO2011119208A1 (en) 2010-03-23 2011-09-29 Ineos Usa Llc Improved mixed metal oxide ammoxidation catalysts
WO2011119206A1 (en) 2010-03-23 2011-09-29 Ineos Usa Llc Attrition resistant mixed metal oxide ammoxidation catalysts
WO2013043371A1 (en) 2011-09-21 2013-03-28 Ineos Usa Llc Mixed metal oxide catalysts
WO2015183284A1 (en) 2014-05-29 2015-12-03 Ineos Usa, Llc Improved selective ammoxidation catalysts
WO2015183283A1 (en) 2014-05-29 2015-12-03 Ineos Usa, Llc Improved selective ammoxidation catalysts
WO2018071166A1 (en) 2016-10-11 2018-04-19 Ineos Europe Ag Ammoxidation catalyst with selective co-product hcn production
US10676426B2 (en) 2017-06-30 2020-06-09 Novomer, Inc. Acrylonitrile derivatives from epoxide and carbon monoxide reagents
WO2023223295A1 (en) 2022-05-20 2023-11-23 Ineos Europe Ag Catalyst for the manufacture of acrylonitrile

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FR1383210A (en) 1964-12-24
CA742727A (en) 1966-09-13

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